Hydroconversion of renewable feedstocks

ABSTRACT

A hydrocarbon conversion process comprises contacting a renewable feedstock under hydroprocessing conditions with supported catalyst comprising at least one metal selected from the group consisting of Group VIII metals, Group VIB metals to form oleochemicals such as fatty alcohols, esters, and normal paraffins. Advantageously, the reaction conditions can be selected to directly convert the renewable feedstock to the desired product(s).

TECHNICAL FIELD

The application relates generally to a process for converting renewablefeedstocks to oleochemicals such as fatty alcohols, esters, and normalparaffins by contacting the feedstock with a supported metal catalystunder hydroprocessing conditions.

BACKGROUND

Fossil fuels are a finite, non-renewable resource formed from decayedplants and animals that have been converted to crude oil, coal, naturalgas, or heavy oils by exposure to heat and pressure in the earth's crustover hundreds of millions of years. However, as the world's petroleumresources are depleting coupled with its ever-increasing prices, manyindustries worldwide have been looking into renewable/sustainable rawmaterials to replace petroleum-based materials in their manufacturingprocesses.

Industrial oleochemicals are useful in the production of surfactants,lubricants, fuels, plastics, and the like. Oleochemicals include, butare not limited to, fatty alcohols, esters and paraffins. Providingefficient processes for directly converting renewable materials intosuch products would be highly desirable.

SUMMARY

In one aspect, there is provided a hydrocarbon conversion processcomprising contacting a renewable feedstock, under hydroprocessingconditions, with a supported catalyst comprising at least one metalselected from the group consisting of Group VIII metals, Group VIBmetals to form an effluent and recovering a fatty alcohol fraction fromthe effluent, wherein the hydroprocessing conditions include atemperature of from 383° F. to 464° F. (195° C. to 240° C.) and a totalreaction pressure of from 800 to 2000 psig (5.5 to 13.8 MPa gauge).

In another aspect, there is provided a hydrocarbon conversion processcomprising contacting a renewable feedstock, under hydroprocessingconditions, with a supported catalyst comprising at least one metalselected from the group consisting of Group VIII metals, Group VIBmetals to form an effluent and recovering an aliphatic monoesterfraction from the effluent, wherein the hydroprocessing conditionsinclude a temperature of from 383° F. to 464° F. (195° C. to 240° C.)and a total reaction pressure of from 800 to 2000 psig (5.5 to 13.8 MPagauge).

In yet another aspect, there is provided hydrocarbon conversion processcomprising contacting a renewable feedstock, under hydroprocessingconditions, with a supported catalyst comprising at least one metalselected from the group consisting of Group VIII metals, Group VIBmetals to form an effluent and recovering a hydrocarbon fractioncomprising normal paraffins from the effluent, wherein thehydroprocessing conditions include a temperature of from 491° F. to 662°F. (255° C. to 350° C.) and a total reaction pressure of from 800 to2000 psig (5.5 to 13.8 MPa gauge).

DETAILED DESCRIPTION

The following terms will be used throughout the specification and willhave the following meanings unless otherwise indicated.

The term “renewable feedstock” is meant to include feedstocks other thanthose obtained from crude oil.

The term “oleochemical” refers to a chemical that isbiologically-derived, i.e., from a renewable resource of biologicalorigin. Such a term is generally accepted as being exclusive of fossilfuels.

A “middle distillate” is a hydrocarbon product having a boiling range offrom 250° F. to 1100° F. (121° C. to 593° C.). The term “middledistillate” includes the diesel, heating oil, jet fuel, and keroseneboiling range fractions. It may also include a portion of naphtha orlight oil. A “jet fuel” is a hydrocarbon product having a boiling rangein the jet fuel boiling range. The term “jet fuel boiling range” refersto hydrocarbons having a boiling range of from 280° F. to 572° F. (138°C. to 300° C.). The term “diesel fuel boiling range” refers tohydrocarbons having a boiling range of from 250° F. to 1000° F. (121° C.to 538° C.). The “boiling range” is the 10 vol. % boiling point to thefinal boiling point (99.5 vol. %), inclusive of the end points, asmeasured by ASTM D2887-08 (“Standard Test Method for Boiling RangeDistribution of Petroleum Fractions by Gas Chromatography”).

The term “triglyceride,” refers to class of molecules having the generalformula (1):

wherein R, R¹ and R² are independently aliphatic residues having from 6to 22 carbon atoms (e.g., from 8 to 20 carbon atoms, or from 10 to 16carbon atoms). The term “aliphatic” means a straight (i.e., un-branched)or branched, substituted or un-substituted hydrocarbon chain that iscompletely saturated or that contains one or more units of unsaturation.

The term “fatty alcohol” refers to primary aliphatic alcohols generallyhaving from 8 to 24 carbon atoms, usually from 8 to 18 carbon atoms.

The term “aliphatic monoester” refers to compounds having the generalformula (2):

wherein R³ and R⁴ are independently alkyl moieties, R⁴ is an alkylmoiety having at least 8 carbon atoms, and the total carbon number ofthe aliphatic monoester is at least 14. In some embodiments, thealiphatic ester has from 16 to 40 carbon atoms (e.g., from 18 to 36, orfrom 20 to 34 carbon atoms). Such esters can be useful as lubricants.

The term “paraffin” refers to any saturated hydrocarbon compound, i.e.,an alkane having the formula C_(n)H_((2n+2)) where n is a positivenon-zero integer.

The term “normal paraffin” refers to a saturated straight chainhydrocarbon.

The term “isoparaffin” refers to a saturated branched chain hydrocarbon.

The term “hydroconversion” can be used interchangeably with the term“hydroprocessing” and refers to any process that is carried out in thepresence of hydrogen and a catalyst. Such processes include, but are notlimited to, methanation, water gas shift reactions, hydrogenation,hydrotreating, hydrodesulfurization, hydrodenitrogenation,hydrodeoxygenation, hydrodemetallation, hydrodeoxygenation,hydrodearomatization, hydroisomerization, hydrodewaxing andhydrocracking including selective hydrocracking.

The term “supported catalyst” refers a catalyst in which the activecomponents, in this case Group VIII and Group VIB metals or compoundsthereof, are deposited on a carrier or support.

When used herein, the Periodic Table of the Elements refers to theversion published by the CRC Press in the CRC Handbook of Chemistry andPhysics, 88th Edition (2007-2008). The names for families of theelements in the Periodic Table are given here in the Chemical AbstractsService (CAS) notation.

The term “isomerizing” refers to catalytic process in which a normalparaffin is converted at least partially into an isoparaffin. Suchisomerization generally proceeds by way of a catalytic route.

The term “conversion” refers to the amount of triglycerides in the feedthat is converted to compounds other than triglycerides. Conversion isexpressed as a weight percentage based on triglycerides in the feed.“Selectivity” is expressed as a weight percent based on convertedtriglycerides. It should be understood that each compound converted fromtriglycerides has an independent selectivity and that selectivity isindependent from conversion.

Feed

The renewable feedstocks that can be used include any of those whichcomprise triglycerides. The feedstock generally originates from abiomass source selected from the group consisting of crops, vegetables,microalgae, animal fats, and combinations thereof. The feedstockgenerally comprises at least 25 wt. % triglycerides (e.g., at least 50wt. %, 75 wt. %, 90 wt. %, or 95 wt. % triglycerides). Those of skill inthe art will recognize that generally any biological source of lipidscan serve as the biomass from which the feedstock can be obtained. Itwill be further appreciated that some such sources are more economicaland more amenable to regional cultivation, and also that those sourcesfrom which food is not derived can be additionally attractive (so as notto be seen as competing with food). Exemplary feedstocks include, butare not limited to canola oil, coconut oil, palm oil, palm kernel oil,peanut oil, rapeseed oil, soybean oil, and the like.

Hydroprocessing Catalyst

Hydrotreating catalysts are suitable for hydroconversion of renewablefeedstocks. Such catalysts comprise at least one metal componentselected from Group VIII metals and/or at least one metal componentselected from the Group VIB metals. Group VIII metals include iron (Fe),cobalt (Co) and nickel (Ni). The noble metals, especially palladium (Pd)and/or platinum (Pt), can be included in the hydrotreating catalyst.Group VIB metals include chromium (Cr), molybdenum (Mo) and tungsten(W). Group VIII metals can present in the catalyst in an amount of from0.5 to 25 wt. % (e.g., from 2 to 20 wt. %, 3 to 10 wt. %, 5 to 10 wt. %,or 5 to 8 wt. %) and Group VIB metals can be present in the catalyst inan amount of from 0.5 to 25 wt. % (e.g., from 5 to 20 wt. %, or 10 to 15wt. %), calculated as metal oxide(s) per 100 parts by weight of totalcatalyst, where the percentages by weight are based on the weight of thecatalyst before sulfiding. The total weight percent of metals employedin the hydrotreating catalyst is at least 15 wt. %. The remainder of thecatalyst can be composed of the support material, although optionallyother components may be present (e.g., filler, cracking component,molecular sieve, or the like, or a combination thereof).

The metal components in the catalyst can be in the oxide and/or thesulfide form. If a combination of at least a Group VIII and a Group VIBmetal component is present as (mixed) oxides, it can be subjected to asulfiding treatment prior to proper use in hydroprocessing. Suitably,the catalyst usually comprises one or more components of Ni and/or Coand one or more components of Mo and/or W.

The hydrotreating catalyst can be prepared by blending, or co-mulling,active sources of the aforementioned metals with a binder. Examples ofbinders include silica, silicon carbide, amorphous and crystallinesilica-aluminas, silica-magnesias, aluminophosphates, boria, titania,zirconia, and the like, as well as mixtures and co-gels thereof.Preferred supports include silica, alumina, alumina-silica, and thecrystalline silica-aluminas, particularly those materials classified asclays or zeolitic materials. Especially preferred support materialsinclude alumina, silica, and alumina-silica, particularly either aluminaor silica. Other components, such as phosphorous, can be added asdesired to tailor the catalyst particles for a desired application. Theblended components can then shaped, such as by extrusion, dried andcalcined at temperatures up to 1200° F. (649° C.) to produce thefinished catalyst. Alternatively, other methods of preparing theamorphous catalyst include preparing oxide binder particles, such as byextrusion, drying and calcining, followed by depositing theaforementioned metals on the oxide particles, using methods such asimpregnation. The catalyst, containing the aforementioned metals, canthen further dried and calcined prior to use as a hydrotreatingcatalyst.

In some such embodiments, the active metal catalyst component isselected from the group consisting of a Ni—Mo catalyst, a Ni—W catalyst,a Ni—Mo—W catalyst, a Co—Mo catalyst, and combinations thereof. In someparticular embodiments, the hydroprocessing step makes use of analumina-supported Ni—Mo catalyst.

In some embodiments, the catalyst is characterized by an average poresize of from 1 to 10 nm (e.g., from 5 to 10 nm) and a surface area offrom 20 to 400 m²/g (e.g., from 100 to 300 m²/g).

Hydroprocessing Conditions

The hydroprocessing conditions can be selected so that an overallconversion rate of triglycerides in the feedstock is at least 50 wt. %,(e.g., at least 60 wt. %, 70 wt. %, 80 wt. %, 90 wt. %, or 95 wt. %).Suitable hydroprocessing conditions can include a temperature of from383° F. to 662° F. (195° C. to 350° C.), e.g., from 383° F. to 464° F.(195° C. to 240° C.), 491° F. to 662° F. (255° C. to 350° C.), or from491° F. to 563° F. (255° C. to 295° C.); a total reaction pressure offrom 500 to 2000 psig (3.4 to 13.8 MPa gauge), e.g., from 800 to 2000psig (5.5 to 13.8 MPa gauge), or from 1600 to 2000 psig (11.0 to 13.8MPa gauge); a liquid hourly space velocity (LHSV) of from 0.1 to 5 h⁻¹,e.g., from 0.5 to 2 h⁻¹; and a hydrogen feed rate of from 0.1 to 20MSCF/bbl (thousand standard cubic feet per barrel), e.g., from 1 to 10MSCF/bbl. Note that a feed rate of 10 MSCF/bbl is equivalent to 1781 LH₂/L feed.

The hydroprocessing process can be single-staged or multiple-staged. Inone embodiment, the process utilizes a single-stage system. Catalystsprepared from the catalyst precursor can be applied in any reactor type.In one embodiment, the catalyst is applied to a fixed bed reactor.

If desired, unreacted triglycerides can be recycled to the reactionsystem for further processing to maximize production of the desiredproduct(s).

Products

The effluent from the hydroprocessing zone will comprise a liquidportion and a gaseous portion. After hydroprocessing, the effluent canbe passed to one or more separators/fractionators for the removal of gasphase products (e.g., CO, CO₂, methane and propane) and separation ofone or more fully and/or partially deoxygenated product fractions (e.g.,n-paraffins, fatty alcohols and/or aliphatic monoesters) from the liquidportion. Different feedstocks will result in different carbondistributions of liquid products.

In one embodiment the liquid product is a product selected from thegroup of a fatty alcohol, an aliphatic monoester, and normal paraffins.In another embodiment, the product is a fatty alcohol, an aliphaticmonoester, or a combination thereof. The hydroprocessing conditions canbe selected from any parameter that influences the subsequent level ofthe desired product(s) in the effluent from the reactor. In one aspect,the hydroprocessing parameter is one that obtains a yield of a productin the reactant mixture, increases the yield of a product, optimizes theselectivity of products in the reactor, or is effective for a conversionof triglycerides in the reactor. In one embodiment, the hydroprocessingparameter is selected from the group consisting of a reactortemperature, a reactor pressure and combinations thereof.

In some embodiments, the effluent comprises a fatty alcohol fraction. Insome embodiments, the effluent comprises at least 20 wt. % of a fattyalcohol (e.g., at least 25 wt. %, 30 wt. %, 30 wt. %, 35 wt. %, 40 wt.%, or 45 wt. % of a fatty alcohol). In some embodiments, the effluenthas a selectivity to a fatty alcohol of at least 30% (e.g., at least35%, 40%, or 45%).

In some embodiments, the effluent comprises an aliphatic monoesterfraction. In some embodiments, the effluent comprises at least 20 wt. %of an aliphatic monoester (e.g., at least 25 wt. % of an aliphaticmonoester). In some embodiments, the effluent has a selectivity to analiphatic monoester of at least 20% (e.g., at least 25%, 30%, 35%, 40%or 45%).

In some embodiments, the effluent comprises a hydrocarbon fractioncomprising normal paraffins. In some embodiments, the effluent comprisesat least 80 wt. % of normal paraffins. In some embodiments, the normalparaffins have from 8 to 24 carbon atoms (e.g., from 12 to 18 carbonatoms).

Note that the normal paraffins can be utilized as a middle distillatefuel. However, subsequent isomerization of the normal paraffins toisoparaffins can provide a broader range of products, thereby making theprocess more universal and flexible.

Catalytic Isomerization

In some embodiments, such above-described processes can further comprisea step of catalytically isomerizing at least some of the normalparaffins to form an isomerized product comprising isoparaffins. In someembodiments, the step of catalytically isomerizing results in superiorfuel properties (e.g., cloud point, pour point etc.) relative to thoseof the non-isomerized paraffinic product.

In some embodiments, the step of isomerizing is carried out using anisomerization catalyst. Suitable such isomerization catalysts caninclude, but are not limited to, Pt and/or Pd on a support. Suitablesupports include, but are not limited to, zeolites CIT-1, IM-5,SSZ-20,SSZ-23, SSZ-24, SSZ-25, SSZ-26, SSZ-31, SSZ-32, SSZ-32, SSZ-33,SSZ-35, SSZ-36, SSZ-37, SSZ-41, SSZ-42, SSZ-43, SSZ-44, SSZ-46, SSZ-47,SSZ-48, SSZ-51, SSZ-56, SSZ-57, SSZ-58, SSZ-59, SSZ-60, SSZ-61, SSZ-63,SSZ-64, SSZ-65, SSZ-67, SSZ-68, SSZ-69, SSZ-70, SSZ-71, SSZ-74, SSZ-75,SSZ-76, SSZ-78, SSZ-81, SSZ-82, SSZ-83, SSZ-86, SUZ-4, TNU-9, ZSM-5,ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-48, EMT-type zeolites, FAU-typezeolites, FER-type zeolites, MEL-type zeolites, MFI-type zeolites,MTT-type zeolites, MTW-type zeolites, MWW-type zeolites, TON-typezeolites, other molecular sieves materials based upon crystallinealuminophosphates such as SM-3, SM-7, SAPO-11, SAPO-31, SAPO-41, MAPO-11and MAPO-31. In some embodiments, the step of isomerizing involves a Ptand/or Pd catalyst supported on an acidic support material selected fromthe group consisting of beta or zeolite Y molecular sieves, silica,alumina, silica-alumina, and combinations thereof. For other suitableisomerization catalysts, see, e.g., U.S. Pat. Nos. 4,859,312; 5,158,665;and 5,300,210.

Isomerization conditions can include a temperature of from 200° F. to900° F. (93° C. to 482° C.), e.g., from 300° F. to 800° F. (149° C. to427° C.), or from 400° F. to 800° F. (204° C. to 427° C.); a totalreaction pressure of from 15 to 3000 psig (0.1 to 20.7 MPa gauge), e.g.,from 50 to 2500 psig (0.3 to 17.2 MPa gauge); a LHSV of from 0.1 to 10h⁻¹, e.g., from 0.25 to 5 h⁻¹; and a hydrogen gas treat rate of from 0.1to 30 MSCF/bbl, e.g., from 0.2 to 20 MSCF/bbl, or from 0.4 to 10MSCF/bbl.

With regard to the catalytic isomerization step described above, in someembodiments, the methods described herein can be conducted by contactingthe normal paraffins with a fixed stationary bed of catalyst, with afixed fluidized bed, or with a transport bed. In one embodiment, atrickle-bed operation is employed, wherein such feed is allowed totrickle through a stationary fixed bed, typically in the presence ofhydrogen. For an illustration of the operation of such catalysts, see,U.S. Pat. Nos. 6,204,426 and 6,723,889.

In some embodiments, the isomerized product comprises at least 10 wt. %isoparaffins (e.g., at least 30 wt. %, 50 wt. %, or 70 wt. %isoparaffins). In some embodiments, the isomerized product has anisoparaffin to normal paraffin mole ratio of at least 5:1 (e.g., atleast 10:1, 15:1, or 20:1).

In some embodiments, the isomerized product has a boiling range of from250° F. to 1100° F. (121° C. to 593° C.), e.g., from 280° F. to 572° F.(138° C. to 300° C.), or from 250° F. to 1000° F. (121° C. to 538° C.).

In some embodiments, the isomerized product is suitable (or bettersuited) for use as a transportation fuel. In some such embodiments, theisomerized product is mixed or admixed with existing transportationfuels in order to create new fuels or to modify the properties ofexisting fuels. Isomerization and blending can be used to modulate andmaintain pour point and cloud point of the fuel or other product atsuitable values. In some embodiments, the normal paraffins are blendedwith other species prior to undergoing catalytic isomerization. In someembodiments, the normal paraffins are blended with the isomerizedproduct.

EXAMPLES

The following illustrative examples are intended to be non-limiting.

Example 1 Soybean Oil Feed

Soybean oil was purchased from Lucky Supermarket (El Cerrito, Calif.)under the Sunny Select brand. The soybean feed had an API gravity of21.6 (0.9223 g/mL). The triglycerides of soybean oil are derived mainlyfrom five fatty acids (see, e.g., D. Firestone, Physical and ChemicalCharacteristics of Oils, Fats, and Waxes, 2^(nd) Edition, 2006, AOCSPress, 149). Table 1 discloses the representative ranges of these fattyacids in soybean oil.

TABLE 1 Fatty acid Carbon atoms:Double bonds Weight Percent Palmiticacid 16:0  9.7 to 13.3 Stearic acid 18:0 3.0 to 5.4 Oleic acid 18:1 17.7to 28.5 Linoleic acid 18:2 49.8 to 57.1 α-Linoleic acid 18:3 5.5 to 9.5

Examples 2-5

The soybean oil feed from Example 1 was tested under hydroprocessingconditions at several temperatures in a single-stage reactor over analumina-supported Ni—Mo catalyst available from Chevron Lummus Global.The catalyst had a median pore size of about 8 nm and specific surfacearea of about 180 m²/g. The reactor conditions include a total reactionpressure of 1900 psig (13.1 MPa gauge), a hydrogen gas rate of 8.0MSCF/bbl, and a LHSV of 1.0 h⁻¹.

The composition of the whole product was determined by gaschromatography (GC) and is set forth in wt. % in Table 2. All liquidparaffinic products were normal paraffins as determined by GC withnegligible amounts of isoparaffins formed. Methane and propane wereessentially the only other hydrocarbon products. Water, carbon monoxide(CO), and carbon dioxide (CO₂) were by-products from hydrodeoxygenation,hydrodecarbonylation and/or hydrodecarboxylation.

TABLE 2 Composition of the Whole Product in Weight Percent Ex. 2 Ex. 3Ex. 4 Ex. 5 Reaction Temperature, ° F. 400 450 500 550 Products, wt. %Unconverted triglycerides 42.4 0.2 <0.5 <0.5 n-C₁₈ paraffin 1.1 14.968.7 69.0 n-C₁₇ paraffin 0.1 1.5 5.3 4.8 n-C₁₆ paraffin 0.3 1.4 8.3 8.5n-C₁₅ paraffin 0 0 0.6 0.5 C₁₈ alcohol 19.6 42.5 — — C₁₆ alcohol 0.5 4.6— — C₁₈ acid 0.4 0.4 — — C₁₆ acid 0 0 — — C₁₈-C₁₈ ester 20.9 16.7 — —C₁₈-C₁₆ ester 5.5 4.0 — — C₁₆-C₁₆ ester 0.4 0.2 — — Unknown heavies 2.71.5 — — Propane 2.8 4.9 4.9 4.9 Methane 0 0 0.1 0.3 H₂O 3.3 7.0 11.411.8 CO 0 0 0 0 CO₂ 0.1 0.3 0.6 0.3

The conversion rate of triglycerides and product selectivity of thehydroprocessing runs are set forth in Table 3.

TABLE 3 Conversion of Triglycerides and Product Selectivity Ex. 2 Ex. 3Ex. 4 Ex. 5 Reaction Temperature, ° F. 400 450 500 550 Conversion of57.6 99.8 >99.5 >99.5 triglycerides, wt. % Product Selectivity, % n-C₁₈paraffin 1.9 15.0 68.7 69.0 n-C₁₇ paraffin 0.1 1.5 5.3 4.8 n-C₁₆paraffin 0.5 1.4 8.3 8.5 n-C₁₅ paraffin 0 0 0.6 0.5 C₁₈ alcohol 34.042.6 — — C₁₆ alcohol 0.8 4.6 — — C₁₈ acid 0.7 0.4 — — C₁₆ acid 0 0 — —C₁₈-C₁₈ ester 36.2 16.7 — — C₁₈-C₁₆ ester 9.5 4.0 — — C₁₆-C₁₆ ester 0.60.2 — — Unknown heavies 4.7 1.5 — — Propane 4.9 4.9 4.9 4.9 Methane 0.10.1 0.1 0.3 H₂O 5.8 7.0 11.4 11.8 CO 0 0 0 0 CO₂ 0.3 0.3 0.6 0.3

For the purposes of this specification and appended claims, unlessotherwise indicated, all numbers expressing quantities, percentages orproportions, and other numerical values used in the specification andclaims, are to be understood as being modified in all instances by theterm “about.” Accordingly, unless indicated to the contrary, thenumerical parameters set forth in the following specification andattached claims are approximations that can vary depending upon thedesired properties sought to be obtained. It is noted that, as used inthis specification and the appended claims, the singular forms “a,”“an,” and “the,” include plural references unless expressly andunequivocally limited to one referent. As used herein, the term“include” and its grammatical variants are intended to be non-limiting,such that recitation of items in a list is not to the exclusion of otherlike items that can be substituted or added to the listed items. As usedherein, the term “comprising” means including elements or steps that areidentified following that term, but any such elements or steps are notexhaustive, and an embodiment can include other elements or steps.

Unless otherwise specified, the recitation of a genus of elements,materials or other components, from which an individual component ormixture of components can be selected, is intended to include allpossible sub-generic combinations of the listed components and mixturesthereof.

The patentable scope is defined by the claims, and can include otherexamples that occur to those skilled in the art. Such other examples areintended to be within the scope of the claims if they have structuralelements that do not differ from the literal language of the claims, orif they include equivalent structural elements with insubstantialdifferences from the literal languages of the claims. To an extent notinconsistent herewith, all citations referred to herein are herebyincorporated by reference.

1. A hydrocarbon conversion process, comprising: a) contacting arenewable feedstock, under hydroprocessing conditions, with a supportedcatalyst comprising at least one metal selected from the groupconsisting of Group VIII metals, Group VIB metals to form an effluent;and b) recovering an aliphatic monoester fraction from the effluent,wherein the hydroprocessing conditions include a temperature of from383° F. to 464° F. (195° C. to 240° C.) and a total reaction pressure offrom 800 to 2000 psig (5.5 to 13.8 MPa gauge).
 2. The process of claim1, having a triglyceride conversion rate of at least 50 wt. %.
 3. Theprocess of claim 1, wherein the feedstock comprises at least 50 wt. %triglycerides.
 4. The process of claim 1, wherein the feedstockoriginates from a biomass source selected from the group consisting ofcrops, vegetables, microalgae, animal fats, and combinations thereof. 5.The process of claim 1, wherein the feedstock is selected from the groupconsisting of canola oil, coconut oil, palm oil, palm kernel oil, peanutoil, rapeseed oil, soybean oil, and combinations thereof.
 6. The processof claim 1, wherein the Group VIII metal is selected from a noble metal,Fe, Co and Ni and the Group VIB metal is selected from the groupconsisting of Cr, Mo and W.
 7. The process of claim 1, wherein thecatalyst is selected from the group consisting of a Ni—Mo catalyst, aNi—W catalyst, a Ni—Mo—W catalyst, a Co—Mo catalyst, and combinationsthereof.
 8. The process of claim 1, wherein the catalyst is analumina-supported Ni—Mo catalyst.
 9. The process of claim 1, wherein thecatalyst has an average pore size of from 1 to 10 nm and a surface areaof from 20 to 400 m²/g.
 10. The process of claim 1, wherein the pressureis from 1600 to 2000 psig (11.0 to 13.8 MPa gauge).
 11. The process ofclaim 1, wherein the effluent comprises at least 20 wt. % of analiphatic monoester.
 12. The process of claim 1, wherein the effluentcomprises at least 25 wt. % of an aliphatic monoester.
 13. The processof claim 1, having an aliphatic monoester selectivity in the effluent ofat least 20%.
 14. The process of claim 1, having an aliphatic monoesterselectivity in the effluent of at least 40%.
 15. The process of claim 1,wherein the aliphatic monoester has from 18 and 36 carbon atoms.